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CN1277095C - Integrated high pressure NGL recovery in prodn. of liquefied natural gas - Google Patents

Integrated high pressure NGL recovery in prodn. of liquefied natural gas Download PDF

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Publication number
CN1277095C
CN1277095C CNB2004100368664A CN200410036866A CN1277095C CN 1277095 C CN1277095 C CN 1277095C CN B2004100368664 A CNB2004100368664 A CN B2004100368664A CN 200410036866 A CN200410036866 A CN 200410036866A CN 1277095 C CN1277095 C CN 1277095C
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Prior art keywords
methane
cooling
rich
logistics
stream
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CNB2004100368664A
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Chinese (zh)
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CN1539930A (en
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M·J·罗伯特斯
H·C·罗勒斯
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Air Products and Chemicals Inc
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Air Products and Chemicals Inc
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    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
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    • F25J1/0217—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process using a multi-component refrigerant [MCR] fluid in a closed vapor compression cycle as at least a three level refrigeration cascade with at least one MCR cycle
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    • F25J2270/00—Refrigeration techniques used
    • F25J2270/12—External refrigeration with liquid vaporising loop
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2270/00—Refrigeration techniques used
    • F25J2270/60—Closed external refrigeration cycle with single component refrigerant [SCR], e.g. C1-, C2- or C3-hydrocarbons
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2270/00—Refrigeration techniques used
    • F25J2270/66—Closed external refrigeration cycle with multi component refrigerant [MCR], e.g. mixture of hydrocarbons
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2290/00—Other details not covered by groups F25J2200/00 - F25J2280/00
    • F25J2290/50—Arrangement of multiple equipments fulfilling the same process step in parallel

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  • Mechanical Engineering (AREA)
  • Thermal Sciences (AREA)
  • General Engineering & Computer Science (AREA)
  • Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Separation By Low-Temperature Treatments (AREA)
  • External Artificial Organs (AREA)
  • Gas Separation By Absorption (AREA)

Abstract

Process for the recovery of components heavier than methane from natural gas, wherein the process comprises (a) cooling a natural gas feed to provide a cooled natural gas feed and introducing the cooled natural gas feed into an absorber column at a first location therein; (b) withdrawing from the absorber column a first overhead vapor stream depleted in components heavier than methane and a bottoms stream enriched in components heavier than methane; (c) introducing a methane-rich reflux stream at a second location in the absorber column above the first location; (d) separating the bottoms stream into a stream enriched in methane and one or more streams enriched in components heavier than ethane; and (e) introducing an absorber liquid comprising components heavier than ethane into the absorber column at a location between the first location and the second location.

Description

Integrated high voltage natural gas liquids recovery method in the liquefied natural gas (LNG) production process
Background technology
Raw gas mainly comprises methane, also comprises numerous submembers, the light hydrocarbon that it can comprise water, hydrogen sulfide, carbon dioxide, mercury, nitrogen and contain 2-6 carbon atom usually simultaneously.In these compositions some are to downstream procedures such as water, hydrogen sulfide, carbon dioxide and mercury, produce harmful impurity such as natural gas processing or liquefied natural gas (LNG), and these impurity must be removed in the upstream of these procedure of processings.The hydrocarbon heavier than methane is condensed usually and reclaims and fractionation obtains valuable hydrocarbon product with the form of natural gas liquids (NGL).
NGL reclaims and uses cooling, partial condensation and fractionating step, and they need a large amount of refrigeration.This refrigeration can be expanded by the merit of pressurized natural gas raw material and the vaporization of gained condensation of hydrocarbons provides.Perhaps or in addition, described refrigeration can be by using refrigerant, provides as the external closed-loop refrigeration of propane.People wish and can reclaim NGL from pressurized natural gas under the situation of not obvious reduction gas pressure.This just makes gas product (such as pipeline gas or LNG) can be in when providing under feed pressure or the condition a little less than feed pressure, thereby does not need the recompression of raw material and/or product.
In order to approach under the feed pressure to reclaim NGL and gas product can drop to minimum with the consumption of refrigeration energy again simultaneously, need improved NGL recovery method.The following description of the present invention provides a kind of improved oil-poor absorption-type NGL recovery method, and this method can operated under the pressure of methane critical pressure, does not wherein need to reduce the feed pressure of natural gas in method.
Summary of the invention
Embodiment of the present invention comprise the method that reclaims the component heavier than methane from natural gas, and wherein said method comprises:
(a) gas material cooling is imported in the absorption tower in primary importance with gas material that cooling is provided and with the gas material of cooling;
(b) from the absorption tower, take out first overhead vapor stream of the depleted in components heavier and be rich in the tower base stream of the component heavier than methane than methane;
(c) will be rich in the reflux stream of methane in being higher than the second place importing absorption tower of primary importance;
(d) tower base stream is separated into logistics and the one or more strands of logistics that is rich in the component heavier that is rich in methane than ethane; With
(e) position of absorption liquid between the primary importance and the second place that will contain than ethane component heavily imports in the absorption tower.
This method can also comprise mixes the whole of the one or more strands of logistics that are rich in the component heavier than ethane in (d) or the reflux stream that wherein is rich in methane arbitrarily among a part and (c).Perhaps, this method can also comprise with the whole of the one or more strands of logistics that are rich in the component heavier in (d) than ethane or wherein arbitrarily a part take out as product stream.Gas material can be under the above pressure of 600psia.
Absorption liquid can comprise the one or more strands of arbitrarily resulting components of logistics that are rich in the component heavier than ethane from (d).Described absorption liquid can comprise 50 moles of hydrocarbon that contain 5 or 5 above carbon atoms more than the %.Perhaps, described absorption liquid can comprise 50 moles of hydrocarbon that contain 4 or 4 above carbon atoms more than the %.In another alternative, described absorption liquid can comprise 50 moles of hydrocarbon that contain 3 or 3 above carbon atoms more than the %.
Absorption liquid can be in importing to the absorption tower before by using the indirect heat exchange cooling of vaporization recirculated coolant, this vaporization recirculated coolant can be a propane.
This method can also comprise first overhead vapor stream cooling or partial condensation forming the two-phase logistics, with this two-phase logistics separate with obtain second overhead vapor stream and (c) in be rich in the reflux stream of methane.The product that second overhead vapor stream can be used as the depleted in components heavier than methane flows back to receipts.(d) in the one or more strands of logistics that are rich in methane whole or wherein arbitrarily a part can before separating the two-phase logistics, mix with first overhead vapor stream.
Be used for the refrigeration of cooling of first overhead vapor stream or partial condensation can be provided by the indirect heat exchange that uses the cooling of evaporation agent, this cooling of evaporation agent can be a multicomponent refrigerant.
This method can also comprise the second overhead vapor stream cooling, condensation and cross cold so that the gas product of liquefaction to be provided.The second overhead vapor stream cooling, condensation and cold excessively required whole refrigeration or a part wherein can be provided by the indirect heat exchange that uses the cooling of evaporation agent, and this cooling of evaporation agent can be a multicomponent refrigerant.
With the second overhead vapor stream cooling, condensation with cross cold required whole refrigeration or a part wherein can be provided by the indirect heat exchange that uses cold refrigerant, this cold refrigerant is that the merit by the nitrogenous refrigerant of compression expands and provides.
Whole or the part wherein of gas material cooling can be provided by the indirect heat exchange that uses one or more strands of cooling of evaporation agent logistics, and this cooling of evaporation agent can be a propane.
This method can also comprise that the indirect heat exchange that comes from the liquid bottoms stream on absorption tower by use provides the part of gas material cooling, thus the tower base stream that obtains vaporizing and it is imported in the absorption tower steam steam to provide.
This method also comprise with the logistics that is rich in methane in (d) cool off, condensation and cross cold so that the product that is rich in methane of liquefaction to be provided.With the logistics that is rich in methane cool off, condensation and cross the whole of cold required refrigeration or parts wherein can be provided by the indirect heat exchange that uses the cooling of evaporation agent.Perhaps, with the logistics that is rich in methane cool off, condensation and cross the whole of cold required refrigeration or parts wherein can be provided by the indirect heat exchange that uses cold refrigerant, this cold refrigerant is that the merit by the nitrogenous refrigerant of compression expands and provides.The product that is rich in methane of liquefaction can combine with the gas product of liquefaction.
Embodiment of the present invention also comprise the system that reclaims the component heavier than methane from natural gas, and wherein said system comprises:
(a) absorption tower that is used for that natural gas is separated into the logistics that is rich in methane and is rich in the logistics of the component heavier than methane;
(b) natural gas cooling is imported to device in the absorption tower with the device of gas material that cooling is provided with the primary importance of gas material on the absorption tower of cooling;
(b) from the absorption tower, take out first overhead vapor stream of the depleted in components heavier and the device of the tower base stream that is rich in the component heavier than methane than methane;
(c) reflux stream that will be rich in methane imports device in the absorption tower in the second place that is higher than primary importance;
(d) tower base stream is separated into logistics and the one or more strands of separator that is rich in the logistics of the component heavier that is rich in methane than ethane; With
(e) position of absorption liquid between the primary importance and the second place that will contain the component heavier than ethane imports to the device in the absorption tower.
This system also comprise with first overhead vapor stream cooling and partial condensation with the device that forms the two-phase logistics with this two-phase logistics is separated to obtain second overhead vapor stream and to be rich in the device of the reflux stream of methane.This system can also comprise main heat exchanger, has the flow channel (described cooling and partial condensation are to be finished by the indirect heat exchange of the multicomponent refrigerant that uses vaporization) that is used for cooling of first overhead vapor stream and partial condensation therein, flow channel with the multicomponent refrigerant that is used for cooled compressed, the pressure that is used to reduce multicomponent refrigerant is with the dropping equipment of the multicomponent refrigerant that obtains vaporizing and be used for distributing at main heat exchanger the device of the multicomponent refrigerant of described vaporization.
This system can also in main heat exchanger, comprise be used in addition with second overhead vapor stream cooling and at least partial condensation with the flow channel of the gas product that obtains liquefaction.In addition, this system can also comprise the product heat exchanger, and wherein, the indirect heat exchange that the gas product of liquefaction is used cold refrigerant further cools off, and described cold refrigerant is that the merit by the nitrogenous refrigerant of compression expands and to provide.
Detailed Description Of The Invention
According to embodiment of the present invention, natural gas liquids (NGL) reclaims from pressurized natural gas by absorption process, wherein Leng Que natural gas feedstream is directed in the absorption tower, partial condensation by the absorption tower overhead stream and condensate turned back to as phegma obtain being rich in the reflux stream of methane in the tower and absorption liquid is imported in the absorption tower in the centre position.This absorption liquid can obtain in the following manner: the liquid tower base stream that is about to come from the absorption tower carry out fractionation with obtain the one or more strands of liquid streams that contain the hydrocarbon heavier than ethane and with in these logistics at least part or all of one logistics return so that absorption liquid to be provided.This absorption liquid is directed in the absorption tower, and it imports the position between importing raw material and importing between the position of the reflux stream that is rich in methane.This NGL recovery method can integrate with natural gas liquefaction so that a part is used for condensation absorption tower overhead materials for the refrigeration that final gas liquefaction is provided.The fractional method that separates the NGL component is preferred for preparing absorption liquid.
In unique accompanying drawing, illustrated an exemplary of the present invention, wherein be used for NGL reclaim the refrigeration produced with LNG by high-level propane refrigeration, use the medium level refrigeration of the mixed cooling medium that contains methane and ethane and the combination of low-level expansion refrigeration to provide.The preliminary treatment gas material that propane refrigeration is used for pressurizeing is cooled to the operating temperature on NGL absorption tower and is used for the mixed cooling medium condensation.Mixed cooling medium is used for and will comes from the overhead vapours cooling of being rich in methane and the condensation on NGL absorption tower and be used for providing the reflux stream that is rich in methane to the top, absorption tower.The gas expansion refrigeration is used for the flash of steam loss that the LNG with condensation crosses when being as cold as sufficient degree with storage pressure that LNG is reduced pressure (be generally and be lower than about 20psia) and drops to minimum.
Can use the refrigerating system or incompatible the recovery with LNG production of set of systems of any other type that refrigeration is provided as NGL.For example, this refrigeration can be provided by the cascade refrigerating system of methane, ethane or ethene and propane, single refrigerating system, the mixed cooling medium refrigerating system of propane precooling or the dual mixed cooling medium refrigerating system of use mixed cooling medium.Various dissimilar gas expansion refrigerations circulations can be incorporated in any of these refrigerating system.Natural gas and/or refrigerant swelling agent; Handle the method logistics of gas or liquid, also can be incorporated in due course in the described refrigerating system.Basic embodiment of the present invention does not also rely on NGL and reclaims the refrigeration type of using in producing with LNG.
In this exemplary embodiment, the pressurized natural gas raw material of having removed acid gas components hydrogen sulfide and carbon dioxide through preliminary treatment in the pipeline 1 in heat exchanger 3 by using the vaporization propane refrigerant heat exchange that provides via pipeline 5 to cool off.Precooling unstripped gas in the pipeline 7 is generally 600-900psia and 60-80 , and further processed removing anhydrated and mercury in treatment system 9.The unstripped gas of this moment mainly comprise methane and low concentration one or more be in C 2-C 5Heavy hydrocarbon in the scope.Be divided into two parts through the pretreated unstripped gas of pre-cold-peace in the pipeline 11, via pipeline 13 and 15, a part of gas of that in the pipeline 13 is successfully cooled off by the vaporization propane refrigerant that is provided via pipeline 23 by the vaporization propane refrigerant that provides via pipeline 19 with in heat exchanger 21 in heat exchanger 17 respectively.Another part gas in the pipeline 15 in heat exchanger 25 by the gasification method logistics that provides via pipeline 27 (below be described) cooling.Cooling raw material in the pipeline 29 combines with the cooling raw material that comes from heat exchanger 21, and the vaporization propane that the feed stream after this combination is provided via pipeline 33 in heat exchanger 31 further cools off.
In the pipeline 35 in conjunction with feed stream, be generally-20 to-40 , on the intermediate point on absorption tower 37 or primary importance by absorption tower 37.This tower is separated into raw material liquid and first overhead vapours that is rich in methane at the bottom of the tower that is rich in heavy hydrocarbon.Liquid takes out via pipeline 27 at the bottom of the part tower, and vaporization in the formerly described heat exchanger 25, the gained vapor stream through pipeline 39 so that the steam that steams in the absorption tower 37 to be provided.Liquid at the bottom of another part tower is described as natural gas liquids (NGL) usually and flows in the NGL fractionator 43 via pipeline 41.Here, NGL is used known fractional method, comprises that dethanizer, depropanizing tower and/or debutanizing tower fractionation obtain two or more hydrocarbon-fractions.In this embodiment, the tower base stream in the pipeline 41 is separated into the light fraction that contains methane and ethane in the pipeline 45, mainly comprises the cut of propane in the pipeline 47, mainly comprises C in the pipeline 49 4Mainly comprise C in the cut of hydrocarbon and the pipeline 51 5Cut with heavy hydrocarbon.If necessary, also can generate the cut that independently is rich in ethane.
A part of C in the pipeline 51 5Take out via pipeline 53 with heavy hydrocarbon, by pump 55 pumpings, in heat exchanger 57, cool off, and return by pipeline 61 by vaporization propane refrigerant via pipeline 59, obtain the absorption liquid in the whereabouts absorption tower 37, it imports the position and is higher than the primary importance that imports raw material via pipeline 35.Absorption liquid is used for absorbing the heavy hydrocarbon that upwards passes through the unstripped gas on absorption tower.Remaining C 5Take out via pipeline 52 with heavy hydrocarbon.
In embodiment optionally, that part of C in the pipeline 49 and 47 4And/or C 3Hydrocarbon can take out and import in the pipeline 53 to form lighter a little absorption liquid.In another embodiment, absorption liquid can comprise C 3And/or C 4Hydrocarbon and do not contain C 5 +Hydrocarbon.Any hydrocarbon liquid that reclaims from NGL fractionator 43 or liquid mixture can be as the absorption liquids in the absorption tower 37.The selection of forming for absorption liquid will be determined according to the rate of recovery of the concrete NGL component of the composition of the final LNG product of hope and hope.
In very large LNG process units, may require a plurality of parallel liquefaction serial equipments, each equipment will comprise pretreatment of raw material and cooling step, absorption tower 37, main heat exchanger 67, LNG subcooler 83 and relevant container and pipeline.General NGL fractionating system can be used for fractionation in the combination NGL of a plurality of gas liquefaction serial equipment condensation logistics.In this embodiment, the absorption liquid that is used for each absorption tower will be provided by this general NGL fractionating system.
Mainly comprise methane and a small amount of ethane, propane and C 5 +The overhead vapours of hydrocarbon is generally-15 to-35 , takes out from the absorption tower by pipeline 63, and cooling and partial condensation in the flow channel 65 of the signal of main heat exchanger 67, and in separation container or backflow oil storage tank 69, be separated into steam and flow with liquid.Liquid stream after the separation mainly comprises methane and the most ethane, propane and the C that come from the 37 tower items of absorption tower 5 +Hydrocarbon takes out from backflow oil storage tank 69 via pipeline 71.So that the phegma that is rich in methane at 37 tops, whereabouts absorption tower to be provided, this phegma imports in the second place this liquid by pump 73 pumpings and the pipeline 75 of flowing through, and the described second place is higher than the primary importance that imports absorption liquids by pipeline 61.
The natural gas (LNG) that second overhead vapours that is rich in methane takes out from backflow oil storage tank 69 by pipeline 77 and cooling and condensation formation are liquefied in the flow channel 79 of the signal of main heat exchanger 67.Temperature flows in the LNG supercooling heat exchanger 83 via pipeline 81 for the liquid of-150 to-180 , and there, this liquid is crossed in the flow channel 85 of signal and is as cold as-180 to-240 .Supercooled liquid enters into product storage tank 91 by steaming in the valve 87 via pipeline 89, and is separated into final LNG product in the pipeline 93 and the residue flash gas in the pipeline 95.
Methane and ethane in the pipeline 45 that reclaims in NGL fractionator 43 cool off and condensation in the flow channel 97 of the signal of main heat exchanger 67, obtain extra fluid product.This fluid product takes out via pipeline 99, and is cold excessively in the flow channel 101 of the signal of LNG subcooler 83, by valve 103 flash distillations, enters into product storage tank 91 to obtain extra LNG product via pipeline 89.
The refrigeration that is used for said method is passable, for example the LPG refrigerant by circulation reaches first or the warmest temperature range, multicomponent liquid refrigerant by circulation reaches second or intermediate temperature range and reach the 3rd or the coldest temperature range by cold gaseous refrigerant.In one embodiment, the LPG refrigerant that is in the several temperature level in pipeline 5,19,23,33 and 57 can be provided by any recycled propane refrigerating system of type known in this field.Other refrigerant, such as propylene or freon can substitute propane be used in first or the warmest temperature range in.
The multicomponent liquid refrigerant of compression can offer main heat exchanger 67 via pipeline 105, and wherein, described refrigerant is cold excessively in the flow channel 107 of signal, by valve 109 flash distillations, and imports in the distributor 113 via pipeline 111.Multicomponent refrigerant is vaporized in main heat exchanger 67 so that refrigeration to be provided therein, and the refrigerant after the vaporization takes out and turn back to (not shown) in refrigerant compression and the condenser system via pipeline 115.The refrigeration that is used for LNG subcooler 83 can be by cold refrigerant, as nitrogen or contain nitrogen mixture and provide via pipeline 117, it in the flow channel 119 of signal heating in subcooler 83, to provide refrigeration.The refrigerant of heating turns back in the compression and gas expansion system (not shown) that cold refrigerant is provided in pipeline 117 via pipeline 121.Perhaps, being used for the refrigeration that NGL reclaims and LNG produces can be provided by the cascade refrigerating system of methane, ethane or ethene and propane, single refrigerating system, the mixed cooling medium refrigerating system of propane precooling or the dual mixed cooling medium refrigerating system of use mixed cooling medium.Various dissimilar gas expansion refrigerations circulations can be incorporated in any of these refrigerating system.
This method is improved oil-poor (C 4-C 6 +) absorption-type NGL recovery method, it utilizes general refrigerating system to produce LNG and reclaims NGL.From unstripped gas, separate the refrigeration of the required medium level of NGL, only account for the sub-fraction of the required whole refrigerations of production LNG as the refrigeration of ethane, ethene or multicomponent refrigerant.
Be used for the process that the methane rich phegma on NGL absorption tower is rich in the absorption tower overhead vapours of methane in cooling and produce, also include in the above-mentioned steam with C 4-C 6 +Most of C of flash distillation when absorption liquid imports in the described tower 4-C 6 +Component.These heavy hydrocarbons are imported the critical pressure that has increased upper column district steam and liquid mixture at the top on absorption tower, and make described tower at obvious high pressure, descend operation such as the critical pressure that is higher than methane (673psia), thereby do not need to reduce the pressure of gas material.The a part of C that in fractionator 43, produces 4-C 6 +Absorption liquid or another kind of heavy hydrocarbon liquid or liquid mixture are chosen wantonly in the flow channel 65 that can mix or be main heat exchanger 67 with the methane rich phegma in pipeline 71 or 75 and are mixed with first vapor stream of top of the tower 63 that comes from absorption tower 37 before or after the cooling.This will further increase the critical pressure of absorption tower overhead vapor and liquid mixture and if necessary, make described tower operate under higher slightly pressure.
This method also utilizes the required fractional method of separation NGL component to generate heavy hydrocarbon (C 4-C 6 +) absorption liquid, this makes NGL to be reclaimed under the situation that does not reduce the gas material flowing pressure.
Operation LNG production equipment can improve the condensation temperature scope of methane rich LNG logistics and significantly be reduced to liquifying method under high as far as possible pressure provides refrigeration required energy.At C 4-C 6 +On the absorption liquid feed points methane rich phegma imported to and also can avoid in the district of NGL absorption tower final LNG product occurring by the heavy hydrocarbon pollution problems.
When not needing NGL to reclaim, this improved oil-poor absorption process also can be used for removing the heavy hydrocarbon with high-solidification point from natural gas feedstream.This will prevent that LNG from producing solidifying and blockage problem under the required low temperature.In this case, fractionation part can, for example only form by debutanizing tower and relevant reboiler and overhead condenser, be used to produce heavy hydrocarbon (C as tower bottom product 5 +) absorption liquid and discharge than light component from cat head.These reclaim than the optional LNG that can be used as of light component.If use C 4 +The heavy hydrocarbon absorption liquid, then the fractionation part can include only depropanizing tower and relevant reboiler and overhead condenser, is used to produce the heavy hydrocarbon (C as tower bottom product 4 +) absorption liquid and discharge than light component from cat head.
Optional, the above-mentioned improved oil-poor absorption process finished natural gas that when operation, can not liquefy.This will make gas material can be used for the processing of NGL recovery and at the gas product that approaches to obtain under the condition of feed pressure purifying, this is favourable when gas product transports with the form of pipeline gas.
In embodiment optionally, raw material will import in the bottom of tower in the absorption tower 37, will not use reboiler 25, and described tower will only be operated with rectification zone.Come from this optionally at the bottom of the tower on absorption tower liquid will in the domethanizing column that boils again, separate as the part of NGL fractionator 43.
Description of drawings
Unique accompanying drawing is the schematic flow diagram that shows embodiment of the present invention.
The specific embodiment
In order to illustrate one embodiment of the invention, said method is carried out the method simulation.With reference to the accompanying drawings, natural gas is carried out preliminary treatment and remove sour gas (CO 2And H 2S) (not shown), to obtain the pretreated raw material in the pipeline 1, flow is 137, the 824lb mole/hour, forming (in mole %) is: nitrogen 3.9%, methane 87.0%, ethane 5.5%, propane 2.0%, butane 0.9%, pentane and heavy hydrocarbon 0.7%, temperature are 98 , and pressure is 890psia.Other be used for removing anhydrate and the preprocess method 9 of mercury before, this raw material is pre-chilled to about 80  in the heat exchanger 3 that the high-level propane refrigerant that is provided by pipeline 5 is provided.
Natural gas in the pipeline 11 propane refrigerant by three kinds of other levels in heat exchanger 17,21 and 31 further is cooled to-27 , and is fed in the NGL absorption tower 37 via pipeline 35.A part of unstripped gas in the pipeline 15 cools off in absorption tower reboiler 25, and the steam that boiled again is via the bottom on pipeline 39 arrival absorption towers 37.Heavy hydrocarbon (the C that comes from fractionator 43 5-C 6 +) absorption liquid, flow be the 5835lb mole/hour, comprise the butane of 0.5 mole of %, the C of the pentane of 42.6 moles of % and 56.9 moles of % 6 +Hydrocarbon, temperature are-27 , and pressure is 847psia, enters into NGL absorption tower 37 via pipeline 61.This absorption liquid enters into absorption tower 37 in the centre position of natural gas feed point and cat head, and wherein absorption liquid absorbs the most of C in pipeline 35 raw materials 3And heavy hydrocarbon.
First overhead vapours that is rich in methane takes out from the NGL absorption tower via pipeline 63, flow be the 131998lb mole/hour, the nitrogen that comprises (mole %) 4.1%, 90.9% methane, 4.4% ethane, 0.2% propane, 0.015% butane, with 0.4% pentane with than heavy hydrocarbon, temperature is-21 , and pressure is 837psia.This overhead vapours is cooled and partial condensation and flowing in the backflow storage tank 69 of-86  and 807psia at the warm end of main heat exchanger 67.Via pipeline 71 with the 5726lb mole/hour flow condensate liquid is taken out, it comprises the nitrogen of (mole %) 1.4%, 74.5% methane, 15.2% ethane, 1.2% propane, 0.2% butane and 7.6% pentane and than heavy hydrocarbon.The liquid of this methane rich via pipeline 75, turns back to the top on NGL absorption tower 37 with the form of reflux by reflux pump 73, is used for absorbing most of C that flash distillation is come out when by pipeline 61 absorption liquid being imported to tower 5 +Hydrocarbon.Main heat exchanger 67 is by the methane-ethane mixed cooling medium refrigeration of the vaporization of passing through pipeline 105 feed, and the refrigerant after the vaporization turns back to (not shown) in compression, cooling and the condenser system via pipeline 115.
The liquid of 37 bottoms, NGL absorption tower takes out via pipeline 41, flow be the 17387lb mole/hour, comprise the methane of (mole %) 24.6%, 15.0% ethane, 15.2% propane, 7.1% butane, with 38.0% pentane and heavy hydrocarbon, temperature is 72 , and pressure is 844psia.Liquid flows in the NGL fractionator 43 at the bottom of this tower, and described fractionation zone comprises dethanizer, depropanizing tower and debutanizing tower and relevant reboiler and overhead condenser (not shown).Dethanizer with the 6896lb mole/hour flow production comprise (mole %) 62.1% methane, 37.8% ethane and 0.1% propane, temperature is-23 , pressure is cat head methane-ethane (C of 450psia 1-C 2) steam product.This methane-ethane steam flows in the main heat exchanger 67 via pipeline 45, is cooled and condensation in the flow channel 97 of signal, and discharges with the form of liquid via pipeline 99.
Liquid overhead product in the depropanizing tower production flow line 47 in the fractionator 43 wherein comprises the propane of 99.5 moles of %, flow be the 2588lb mole/hour, temperature is 120 , pressure is 245psia.The liquid overhead materials that debutanizing tower in the fractionator 43 is produced is discharged via pipeline 49, comprises the butane of 95 moles of %, flow be the 1269lb mole/hour, temperature is 113 , pressure is 78psia.Debutanizing tower also with the 6634lb mole/hour flow produce C 5 +Liquid tower bottom product, it comprises the butane of 0.5 mole of %, the C of the pentane of 42.6 moles of % and 56.9 moles of % 6 +Hydrocarbon, temperature are 98 , and pressure is 83psia.This C of a part 5 +Liquid bottoms with the 799lb mole/hour flow take out with the form of product via pipeline 52, remainder then via pipeline 53 and pump 55 with the 5838lb mole/hour flow discharge.This logistics is cooled to-27  by the propane refrigerant via pipeline 59 feed in heat exchanger 57, cooled logistics flows in the NGL absorption tower 37 via pipeline 61 as previously mentioned, as the absorption liquid on NGL absorption tower 37.
Second overhead vapours that comes from backflow oil storage tank 69 via pipeline 77 with the 126272lb mole/hour flow discharge, it comprises the nitrogen of (mole %) 4.3%, 91.6% methane, 3.9% ethane, 0.1% propane and 0.1% butane and heavy hydrocarbon, temperature is-86 , and pressure is 807psia.This steam flows in the main heat exchanger 67, there, cooling and all condensations in the flow channel 79 of signal, temperature is-177 middle liquefied natural gas (LNG) product in the formation pipeline 81.This intermediate liquid product is crossed in the signal flow channel 85 of LNG subcooler 83 and is as cold as-237 , is 15.2psia by valve 87 flash distillations, and flows in the final product separator 91 by pipeline 89.Liquid in the other pipeline 99 (before described) is cold excessively in the signal flow channel 101 of LNG subcooler 83, by valve 103 flash distillations, also flows in the final product separator 91 via pipeline 89.Final LNG product is discharged via pipeline 93 and is stored, and flash gas is then discharged via pipeline 95, and use acts as a fuel.The refrigeration of LNG subcooler 83 is provided by the cooling nitrogen refrigerant in the pipeline 117, it warms in the flow channel 119 of signal, and the nitrogen that warms takes out and turns back in compression and the merit expansion system (not shown) so that the nitrogen refrigerant of reuse is provided via pipeline 117 via pipeline 121.
This exemplary method reclaims in the gas material 92.5% propane, 98.6% butane and 99.6% C with the form of NGL product 6And heavier hydrocarbon.The refrigeration that is used for the NGL separation method is the part of the refrigeration that provided for product of natural gas liquefaction.In this embodiment, nearly 74% pentane reclaims with the form of NGL product in the unstripped gas, and this amount is enough to reduce the concentration in the methane rich LNG product, freezes and stop up the cool equipment in 37 downstreams, absorption tower to prevent hydrocarbon.If desired, get back to the C that is mainly in the NGL absorption tower 37 by increasing via pipeline 61 5 +The flow of absorption liquid can improve the rate of recovery of propane, still, this also will need correspondingly to increase the flow of getting back to the methane rich phegma at 37 tops, absorption tower via pipeline 75.To increase the amount of the required medium level refrigeration of this method via pipeline 61 absorption liquid of getting back to NGL absorption tower 37 and the flow increase of getting back to the methane rich phegma on NGL absorption tower 37 via pipeline 75, this refrigeration is to be provided by the methane-propane mixed cooling medium by pipeline 105 in this embodiment.
If mainly with C 4If hydrocarbon is as absorption liquid or with C 4Hydrocarbon joins the C of this embodiment 5-C 6 +In the absorption liquid, C then 5The rate of recovery of hydrocarbon will increase, but in the pipeline 49 as the C of NGL product 4The rate of recovery of hydrocarbon will reduce.Optional, as propane can be provided via pipeline 61 as at least a portion absorption liquid, but this will obviously reduce via the rate of recovery of pipeline 47 as the propane of final products recovery.The selection of forming for absorption liquid can be when reclaiming as the NGL product than heavy hydrocarbon the value decision, this value is with respect to it for value during as final LNG product a part of.The absorption liquid that provides via pipeline 61 can be the heavy hydrocarbon liquid of production in the NGL fractionator 43 or any combination of its liquid mixture.

Claims (31)

1. method that from natural gas, reclaims the component heavier than methane, wherein said method comprises:
(a) gas material cooling is imported in the absorption tower in primary importance with gas material that cooling is provided and with the gas material of cooling;
(b) from the absorption tower, take out first overhead vapor stream of the depleted in components heavier and be rich in the tower base stream of the component heavier than methane than methane;
(c) will be rich in the reflux stream of methane in being higher than the second place importing absorption tower of primary importance;
(d) tower base stream is separated into logistics and the one or more strands of logistics that is rich in the component heavier that is rich in methane than ethane; With
(e) position of absorption liquid between the primary importance and the second place that will contain than ethane component heavily imports in the absorption tower.
2. the method for claim 1 also comprises the whole of the one or more strands of logistics that are rich in the component heavier than ethane in (d) or the reflux stream that wherein is rich in methane arbitrarily among a part and (c) is mixed.
3. the method for claim 1 also comprises one or more strands of the whole or wherein a part of arbitrarily of logistics of being rich in the component heavier than ethane in (d) is taken out as product stream.
4. the process of claim 1 wherein that gas material pressure is more than the 600psia.
5. the process of claim 1 wherein that absorption liquid comprises the one or more strands of arbitrarily resulting components of logistics that are rich in the component heavier than ethane from (d).
6. the process of claim 1 wherein that absorption liquid comprises 50 moles of hydrocarbon that contain 5 or 5 above carbon atoms more than the %.
7. the process of claim 1 wherein that absorption liquid comprises 50 moles of hydrocarbon that contain 4 or 4 above carbon atoms more than the %.
8. the process of claim 1 wherein that absorption liquid comprises 50 moles of hydrocarbon that contain 3 or 3 above carbon atoms more than the %.
9. the process of claim 1 wherein and cooled off by the indirect heat exchange that uses the recirculated coolant of vaporizing before absorption liquid is in importing to the absorption tower.
10. the method for claim 9, the recirculated coolant of wherein said vaporization is a propane.
11. the method for claim 1 also comprises first overhead vapor stream cooling and partial condensation forming the two-phase logistics, with this two-phase logistics separate with obtain second overhead vapor stream with (c) in be rich in the reflux stream of methane.
12. the method for claim 11, wherein second overhead vapor stream flows back to receipts as the product of the depleted in components heavier than methane.
13. the method for claim 11 also comprises one or more strands of the whole or wherein a part of arbitrarily of logistics of being rich in methane in (d) was mixed with first overhead stream before separating the two-phase logistics.
14. the method for claim 11 wherein is used for the refrigeration of cooling of first overhead vapor stream or partial condensation is provided by the indirect heat exchange that uses the cooling of evaporation agent.
15. the method for claim 14, wherein said cooling of evaporation agent is a multicomponent refrigerant.
16. the method for claim 11 also comprises the second overhead vapor stream cooling, condensation and excessively cold so that the gas product of liquefaction to be provided.
17. the method for claim 16 is wherein provided the second overhead vapor stream cooling, condensation and cold excessively required whole refrigeration or a part wherein by the indirect heat exchange that uses the cooling of evaporation agent.
18. the method for claim 17, wherein said cooling of evaporation agent is a multicomponent refrigerant.
19. the method for claim 16, wherein with the second overhead vapor stream cooling, condensation with cross cold required whole refrigeration or a part is wherein provided by the indirect heat exchange that uses cold refrigerant, this cold refrigerant is that the merit by the nitrogenous refrigerant of compression expands and provides.
20. the process of claim 1 wherein that the whole or part wherein of gas material cooling is provided by the indirect heat exchange that uses one or more strands of cooling of evaporation agent logistics.
21. the method for claim 20, wherein said cooling of evaporation agent is a propane.
22. the method for claim 1 comprises that also the indirect heat exchange that comes from the liquid bottoms stream on absorption tower by use provides the part of gas material cooling, thereby the tower base stream that obtains vaporizing and it is imported in the absorption tower steam steam to provide.
23. the method for claim 16, also comprise with the logistics that is rich in methane in (d) cool off, condensation and cross cold so that the product that is rich in methane of liquefaction to be provided.
24. the method for claim 23, the logistics that wherein will be rich in methane is cooled off, condensation and a whole or part wherein of crossing cold required refrigeration are provided by the indirect heat exchange that uses the cooling of evaporation agent.
25. the method for claim 23, the logistics that wherein will be rich in methane is cooled off, condensation and a whole or part wherein of crossing cold required refrigeration are provided by the indirect heat exchange that uses cold refrigerant, and this cold refrigerant is that the merit by the nitrogenous refrigerant of compression expands and provides.
26. the method for claim 23, wherein Ye Hua the product that is rich in methane combines with the gas product of liquefaction.
27. a system that reclaims the component heavier than methane from natural gas, wherein said system comprises:
(a) absorption tower that is used for that natural gas is separated into the logistics that is rich in methane and is rich in the logistics of the component heavier than methane;
(b) gas material cooling is imported to device in the absorption tower with the cooling device of gas material that cooling is provided with the primary importance of gas material on the absorption tower of cooling;
(b) from the absorption tower, take out first overhead vapor stream of the depleted in components heavier and the device of the tower base stream that is rich in the component heavier than methane than methane;
(c) reflux stream that will be rich in methane imports device in the absorption tower in the second place that is higher than primary importance;
(d) tower base stream is separated into logistics and the one or more strands of separator that is rich in the logistics of the component heavier that is rich in methane than ethane; With
(e) position of absorption liquid between the primary importance and the second place that will contain the component heavier than ethane imports to the device in the absorption tower.
28. the system of claim 27, also comprise with first overhead vapor stream cooling and partial condensation with the device that forms the two-phase logistics with this two-phase logistics is separated to obtain second overhead vapor stream and to be rich in the device of the reflux stream of methane.
29. the system of claim 28, also comprise main heat exchanger, have therein and be used for first overhead vapor stream by the indirect heat exchange cooling of the multicomponent refrigerant that uses vaporization and the flow channel of partial condensation, flow channel with the multicomponent refrigerant that is used for cooled compressed, the pressure that is used to reduce multicomponent refrigerant is with the dropping equipment of the multicomponent refrigerant that obtains vaporizing and be used for distributing at main heat exchanger the device of the multicomponent refrigerant of described vaporization.
30. the system of claim 29, also be included in the main heat exchanger be used in addition with second overhead vapor stream cooling and at least partial condensation with the flow channel of the gas product that obtains liquefaction.
31. the system of claim 30 also comprises the product heat exchanger, wherein, the indirect heat exchange that the gas product of liquefaction is used cold refrigerant further cools off, and described cold refrigerant is that the merit by the nitrogenous refrigerant of compression expands and to provide.
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Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN103265987A (en) * 2013-06-05 2013-08-28 中国石油集团工程设计有限责任公司 Process device and method for removing heavy hydrocarbon in natural gas by adopting LPG (Liquefied Petroleum Gas)

Families Citing this family (102)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US7310971B2 (en) * 2004-10-25 2007-12-25 Conocophillips Company LNG system employing optimized heat exchangers to provide liquid reflux stream
FR2855526B1 (en) 2003-06-02 2007-01-26 Technip France METHOD AND INSTALLATION FOR THE SIMULTANEOUS PRODUCTION OF A NATURAL GAS THAT CAN BE LIQUEFIED AND A CUTTING OF NATURAL GAS LIQUIDS
US7278281B2 (en) * 2003-11-13 2007-10-09 Foster Wheeler Usa Corporation Method and apparatus for reducing C2 and C3 at LNG receiving terminals
US20050279132A1 (en) * 2004-06-16 2005-12-22 Eaton Anthony P LNG system with enhanced turboexpander configuration
US7866184B2 (en) * 2004-06-16 2011-01-11 Conocophillips Company Semi-closed loop LNG process
US7600395B2 (en) * 2004-06-24 2009-10-13 Conocophillips Company LNG system employing refluxed heavies removal column with overhead condensing
ATE546508T1 (en) 2005-03-16 2012-03-15 Fuelcor Llc SYSTEMS AND METHODS FOR PRODUCING SYNTHETIC HYDROCARBON COMPOUNDS
US20070061950A1 (en) * 2005-03-29 2007-03-22 Terry Delonas Lipowear
WO2006115597A2 (en) * 2005-04-20 2006-11-02 Fluor Technologies Corporation Integrated ngl recovery and lng liquefaction
US20060260330A1 (en) 2005-05-19 2006-11-23 Rosetta Martin J Air vaporizor
US20060260355A1 (en) * 2005-05-19 2006-11-23 Roberts Mark J Integrated NGL recovery and liquefied natural gas production
US20070012072A1 (en) * 2005-07-12 2007-01-18 Wesley Qualls Lng facility with integrated ngl extraction technology for enhanced ngl recovery and product flexibility
US20070056318A1 (en) * 2005-09-12 2007-03-15 Ransbarger Weldon L Enhanced heavies removal/LPG recovery process for LNG facilities
US20070107464A1 (en) * 2005-11-14 2007-05-17 Ransbarger Weldon L LNG system with high pressure pre-cooling cycle
US7530236B2 (en) * 2006-03-01 2009-05-12 Rajeev Nanda Natural gas liquid recovery
DE102006021620B4 (en) 2006-05-09 2019-04-11 Linde Ag Pretreatment of a liquefied natural gas stream
AU2007251667B2 (en) 2006-05-15 2010-07-08 Shell Internationale Research Maatschappij B.V. Method and apparatus for liquefying a hydrocarbon stream
AU2007267116B2 (en) * 2006-05-30 2010-08-12 Shell Internationale Research Maatschappij B.V. Method for treating a hydrocarbon stream
US20080016910A1 (en) * 2006-07-21 2008-01-24 Adam Adrian Brostow Integrated NGL recovery in the production of liquefied natural gas
RU2447382C2 (en) * 2006-08-17 2012-04-10 Шелл Интернэшнл Рисерч Маатсхаппий Б.В. Method and device for liquefaction of hydrocarbon-containing raw materials flow
US20080098770A1 (en) * 2006-10-31 2008-05-01 Conocophillips Company Intermediate pressure lng refluxed ngl recovery process
AU2007319977B2 (en) * 2006-11-09 2011-03-03 Fluor Technologies Corporation Configurations and methods for gas condensate separation from high-pressure hydrocarbon mixtures
US20080134717A1 (en) * 2006-11-14 2008-06-12 Willem Dam Method and apparatus for cooling a hydrocarbon stream
US8650906B2 (en) * 2007-04-25 2014-02-18 Black & Veatch Corporation System and method for recovering and liquefying boil-off gas
US8783061B2 (en) * 2007-06-12 2014-07-22 Honeywell International Inc. Apparatus and method for optimizing a natural gas liquefaction train having a nitrogen cooling loop
FR2917489A1 (en) * 2007-06-14 2008-12-19 Air Liquide METHOD AND APPARATUS FOR CRYOGENIC SEPARATION OF METHANE RICH FLOW
NO329177B1 (en) * 2007-06-22 2010-09-06 Kanfa Aragon As Process and system for forming liquid LNG
FR2923001B1 (en) * 2007-10-26 2015-12-11 Inst Francais Du Petrole METHOD FOR LIQUEFACTING A NATURAL GAS WITH HIGH PRESSURE FRACTIONATION
US9377239B2 (en) * 2007-11-15 2016-06-28 Conocophillips Company Dual-refluxed heavies removal column in an LNG facility
WO2009076357A1 (en) * 2007-12-10 2009-06-18 Conocophillps Company Optimized heavies removal system in an lng facility
US20090151391A1 (en) * 2007-12-12 2009-06-18 Conocophillips Company Lng facility employing a heavies enriching stream
DE102008004077A1 (en) * 2008-01-12 2009-07-23 Man Diesel Se Process and apparatus for the treatment of natural gas for use in a gas engine
WO2009101127A2 (en) 2008-02-14 2009-08-20 Shell Internationale Research Maatschappij B.V. Method and apparatus for cooling a hydrocarbon stream
US9243842B2 (en) * 2008-02-15 2016-01-26 Black & Veatch Corporation Combined synthesis gas separation and LNG production method and system
GB0812699D0 (en) * 2008-07-11 2008-08-20 Johnson Matthey Plc Apparatus and process for treating offshore natural gas
US9151537B2 (en) * 2008-12-19 2015-10-06 Kanfa Aragon As Method and system for producing liquefied natural gas (LNG)
US8627681B2 (en) * 2009-03-04 2014-01-14 Lummus Technology Inc. Nitrogen removal with iso-pressure open refrigeration natural gas liquids recovery
US20120060552A1 (en) * 2009-05-18 2012-03-15 Carolus Antonius Cornelis Van De Lisdonk Method and apparatus for cooling a gaseous hydrocarbon stream
US10082331B2 (en) * 2009-07-16 2018-09-25 Conocophillips Company Process for controlling liquefied natural gas heating value
US9046302B2 (en) 2009-10-27 2015-06-02 Shell Oil Company Apparatus and method for cooling and liquefying a fluid
US10113127B2 (en) 2010-04-16 2018-10-30 Black & Veatch Holding Company Process for separating nitrogen from a natural gas stream with nitrogen stripping in the production of liquefied natural gas
US20120000242A1 (en) * 2010-04-22 2012-01-05 Baudat Ned P Method and apparatus for storing liquefied natural gas
US20110259044A1 (en) * 2010-04-22 2011-10-27 Baudat Ned P Method and apparatus for producing liquefied natural gas
WO2012003358A2 (en) * 2010-07-01 2012-01-05 Black & Veatch Corporation Methods and systems for recovering liquified petroleum gas from natural gas
AU2011274797B2 (en) * 2010-07-09 2015-05-21 Arnold Keller Carbon dioxide capture and liquefaction
US8635885B2 (en) * 2010-10-15 2014-01-28 Fluor Technologies Corporation Configurations and methods of heating value control in LNG liquefaction plant
CA2819128C (en) * 2010-12-01 2018-11-13 Black & Veatch Corporation Ngl recovery from natural gas using a mixed refrigerant
EP2597407A1 (en) * 2011-11-23 2013-05-29 Shell Internationale Research Maatschappij B.V. Method and apparatus for preparing a lean methane-containing gas stream
CA2763081C (en) 2011-12-20 2019-08-13 Jose Lourenco Method to produce liquefied natural gas (lng) at midstream natural gas liquids (ngls) recovery plants.
US10139157B2 (en) 2012-02-22 2018-11-27 Black & Veatch Holding Company NGL recovery from natural gas using a mixed refrigerant
CA2772479C (en) 2012-03-21 2020-01-07 Mackenzie Millar Temperature controlled method to liquefy gas and a production plant using the method.
CA2790961C (en) 2012-05-11 2019-09-03 Jose Lourenco A method to recover lpg and condensates from refineries fuel gas streams.
MY176383A (en) * 2012-08-03 2020-08-04 Air Prod & Chem Heavy hydrocarbon removal from a natural gas stream
CA2787746C (en) 2012-08-27 2019-08-13 Mackenzie Millar Method of producing and distributing liquid natural gas
CA2798057C (en) 2012-12-04 2019-11-26 Mackenzie Millar A method to produce lng at gas pressure letdown stations in natural gas transmission pipeline systems
US9803917B2 (en) 2012-12-28 2017-10-31 Linde Engineering North America, Inc. Integrated process for NGL (natural gas liquids recovery) and LNG (liquefaction of natural gas)
CA2813260C (en) 2013-04-15 2021-07-06 Mackenzie Millar A method to produce lng
US10563913B2 (en) 2013-11-15 2020-02-18 Black & Veatch Holding Company Systems and methods for hydrocarbon refrigeration with a mixed refrigerant cycle
US9574822B2 (en) 2014-03-17 2017-02-21 Black & Veatch Corporation Liquefied natural gas facility employing an optimized mixed refrigerant system
DE102014005936A1 (en) * 2014-04-24 2015-10-29 Linde Aktiengesellschaft Process for liquefying a hydrocarbon-rich fraction
WO2016023098A1 (en) 2014-08-15 2016-02-18 1304338 Alberta Ltd. A method of removing carbon dioxide during liquid natural gas production from natural gas at gas pressure letdown stations
US20160187057A1 (en) * 2014-12-23 2016-06-30 Aspen Engineering Services, Llc Liquefied natural gas from rich natural gas
US20160216030A1 (en) 2015-01-23 2016-07-28 Air Products And Chemicals, Inc. Separation of Heavy Hydrocarbons and NGLs from Natural Gas in Integration with Liquefaction of Natural Gas
US10928128B2 (en) * 2015-05-04 2021-02-23 GE Oil & Gas, Inc. Preparing hydrocarbon streams for storage
EP3115721A1 (en) 2015-07-10 2017-01-11 Shell Internationale Research Maatschappij B.V. Method and system for cooling and separating a hydrocarbon stream
TWI603044B (en) 2015-07-10 2017-10-21 艾克頌美孚上游研究公司 System and method for producing liquefied nitrogen using liquefied natural gas
TWI606221B (en) 2015-07-15 2017-11-21 艾克頌美孚上游研究公司 Liquefied natural gas production system and method with greenhouse gas removal
TWI608206B (en) 2015-07-15 2017-12-11 艾克頌美孚上游研究公司 Increasing efficiency in an lng production system by pre-cooling a natural gas feed stream
FR3039080B1 (en) * 2015-07-23 2019-05-17 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude METHOD OF PURIFYING HYDROCARBON-RICH GAS
WO2017045055A1 (en) 2015-09-16 2017-03-23 1304342 Alberta Ltd. A method of preparing natural gas at a gas pressure reduction stations to produce liquid natural gas (lng)
EP3390941A1 (en) 2015-12-14 2018-10-24 Exxonmobil Upstream Research Company Method and system for separating nitrogen from liquefied natural gas using liquefied nitrogen
AU2016372711B2 (en) 2015-12-14 2019-05-02 Exxonmobil Upstream Research Company Method of natural gas liquefaction on LNG carriers storing liquid nitrogen
CA2949012C (en) * 2016-01-22 2018-02-20 Encana Corporation Process and apparatus for processing a hydrocarbon gas stream
US11668522B2 (en) 2016-07-21 2023-06-06 Air Products And Chemicals, Inc. Heavy hydrocarbon removal system for lean natural gas liquefaction
US11402155B2 (en) * 2016-09-06 2022-08-02 Lummus Technology Inc. Pretreatment of natural gas prior to liquefaction
US10365038B2 (en) * 2016-09-15 2019-07-30 Lummus Technology Inc. Process for the production of dilute ethylene
FR3056223B1 (en) * 2016-09-20 2020-05-01 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude PROCESS FOR THE PURIFICATION OF NATURAL LIQUEFIED GAS
SG11201906786YA (en) 2017-02-24 2019-09-27 Exxonmobil Upstream Res Co Method of purging a dual purpose lng/lin storage tank
FR3066491B1 (en) * 2017-05-18 2019-07-12 Technip France PROCESS FOR RECOVERING A C2 + HYDROCARBON CURRENT IN A REFINERY RESIDUAL GAS AND ASSOCIATED INSTALLATION
EP3694959A4 (en) * 2017-09-06 2021-09-08 Linde Engineering North America Inc. Methods for providing refrigeration in natural gas liquids recovery plants
US10619917B2 (en) * 2017-09-13 2020-04-14 Air Products And Chemicals, Inc. Multi-product liquefaction method and system
US11236941B2 (en) * 2017-12-15 2022-02-01 Saudi Arabian Oil Company Process integration for natural gas liquid recovery
EP3803241B1 (en) 2018-06-07 2022-09-28 ExxonMobil Upstream Research Company Pretreatment and pre-cooling of natural gas by high pressure compression and expansion
CN111433329A (en) * 2018-07-24 2020-07-17 日挥环球株式会社 Natural gas processing device and natural gas processing method
JP7100762B2 (en) 2018-08-14 2022-07-13 エクソンモービル アップストリーム リサーチ カンパニー Preservation method of mixed refrigerant in natural gas liquefaction facility
US11506454B2 (en) 2018-08-22 2022-11-22 Exxonmobile Upstream Research Company Heat exchanger configuration for a high pressure expander process and a method of natural gas liquefaction using the same
JP7179155B2 (en) 2018-08-22 2022-11-28 エクソンモービル アップストリーム リサーチ カンパニー Primary loop start-up method for high pressure expander process
CA3109918C (en) 2018-08-22 2023-05-16 Exxonmobil Upstream Research Company Managing make-up gas composition variation for a high pressure expander process
WO2020106394A1 (en) 2018-11-20 2020-05-28 Exxonmobil Upstream Research Company Poly refrigerated integrated cycle operation using solid-tolerant heat exchangers
US11215410B2 (en) 2018-11-20 2022-01-04 Exxonmobil Upstream Research Company Methods and apparatus for improving multi-plate scraped heat exchangers
US11668524B2 (en) 2019-01-30 2023-06-06 Exxonmobil Upstream Research Company Methods for removal of moisture from LNG refrigerant
WO2020159671A1 (en) 2019-01-30 2020-08-06 Exxonmobil Upstream Research Company Methods for removal of moisture from lng refrigerant
CN110118468B (en) * 2019-05-10 2020-02-11 西南石油大学 Ethane recovery method with self-cooling circulation and suitable for rich gas
US11465093B2 (en) 2019-08-19 2022-10-11 Exxonmobil Upstream Research Company Compliant composite heat exchangers
US20210063083A1 (en) 2019-08-29 2021-03-04 Exxonmobil Upstream Research Company Liquefaction of Production Gas
EP4031822A1 (en) 2019-09-19 2022-07-27 Exxonmobil Upstream Research Company (EMHC-N1-4A-607) Pretreatment and pre-cooling of natural gas by high pressure compression and expansion
WO2021055021A1 (en) 2019-09-19 2021-03-25 Exxonmobil Upstream Research Company Pretreatment and pre-cooling of natural gas by high pressure compression and expansion
JP7326485B2 (en) 2019-09-19 2023-08-15 エクソンモービル・テクノロジー・アンド・エンジニアリング・カンパニー Pretreatment, pre-cooling and condensate recovery of natural gas by high pressure compression and expansion
US11083994B2 (en) 2019-09-20 2021-08-10 Exxonmobil Upstream Research Company Removal of acid gases from a gas stream, with O2 enrichment for acid gas capture and sequestration
JP2022548529A (en) 2019-09-24 2022-11-21 エクソンモービル アップストリーム リサーチ カンパニー Cargo stripping capabilities for dual-purpose cryogenic tanks on ships or floating storage units for LNG and liquid nitrogen
US10894929B1 (en) 2019-10-02 2021-01-19 Saudi Arabian Oil Company Natural gas liquids recovery process
CN114717031A (en) * 2021-01-05 2022-07-08 中国石油化工股份有限公司 Method for removing nitrogen from natural gas by using low-temperature mixed solvent

Family Cites Families (40)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3313724A (en) * 1965-03-29 1967-04-11 Lummus Co Process for the separation of normally gaseous hydrocarbon mixtures
US3622504A (en) 1969-01-10 1971-11-23 Hydrocarbon Research Inc Separation of heavier hydrocarbons from natural gas
DE1939114B2 (en) 1969-08-01 1979-01-25 Linde Ag, 6200 Wiesbaden Liquefaction process for gases and gas mixtures, in particular for natural gas
US3763658A (en) 1970-01-12 1973-10-09 Air Prod & Chem Combined cascade and multicomponent refrigeration system and method
US3926742A (en) * 1972-03-06 1975-12-16 Phillips Petroleum Co Controlled fractionation method and apparatus
DE2438443C2 (en) 1974-08-09 1984-01-26 Linde Ag, 6200 Wiesbaden Process for liquefying natural gas
CA1021254A (en) 1974-10-22 1977-11-22 Ortloff Corporation (The) Natural gas processing
US4155729A (en) 1977-10-20 1979-05-22 Phillips Petroleum Company Liquid flash between expanders in gas separation
US4203741A (en) 1978-06-14 1980-05-20 Phillips Petroleum Company Separate feed entry to separator-contactor in gas separation
US4203742A (en) 1978-10-31 1980-05-20 Stone & Webster Engineering Corporation Process for the recovery of ethane and heavier hydrocarbon components from methane-rich gases
US4272269A (en) 1979-11-23 1981-06-09 Fluor Corporation Cryogenic expander recovery process
US4445917A (en) 1982-05-10 1984-05-01 Air Products And Chemicals, Inc. Process for liquefied natural gas
US4445916A (en) 1982-08-30 1984-05-01 Newton Charles L Process for liquefying methane
US4504296A (en) 1983-07-18 1985-03-12 Air Products And Chemicals, Inc. Double mixed refrigerant liquefaction process for natural gas
US4657571A (en) 1984-06-29 1987-04-14 Snamprogetti S.P.A. Process for the recovery of heavy constituents from hydrocarbon gaseous mixtures
FR2571129B1 (en) 1984-09-28 1988-01-29 Technip Cie PROCESS AND PLANT FOR CRYOGENIC FRACTIONATION OF GASEOUS LOADS
DE3528071A1 (en) 1985-08-05 1987-02-05 Linde Ag METHOD FOR DISASSEMBLING A HYDROCARBON MIXTURE
US4687499A (en) 1986-04-01 1987-08-18 Mcdermott International Inc. Process for separating hydrocarbon gas constituents
US4809154A (en) 1986-07-10 1989-02-28 Air Products And Chemicals, Inc. Automated control system for a multicomponent refrigeration system
DE3802553C2 (en) 1988-01-28 1996-06-20 Linde Ag Process for the separation of hydrocarbons
US4889545A (en) 1988-11-21 1989-12-26 Elcor Corporation Hydrocarbon gas processing
US4851020A (en) 1988-11-21 1989-07-25 Mcdermott International, Inc. Ethane recovery system
FR2681859B1 (en) 1991-09-30 1994-02-11 Technip Cie Fse Etudes Const NATURAL GAS LIQUEFACTION PROCESS.
US5325673A (en) 1993-02-23 1994-07-05 The M. W. Kellogg Company Natural gas liquefaction pretreatment process
US5345772A (en) * 1993-05-14 1994-09-13 Process Systems International, Inc. Single column distillative separation employing bottom additives
US5568737A (en) 1994-11-10 1996-10-29 Elcor Corporation Hydrocarbon gas processing
CA2223042C (en) 1995-06-07 2001-01-30 Elcor Corporation Hydrocarbon gas processing
US5799507A (en) 1996-10-25 1998-09-01 Elcor Corporation Hydrocarbon gas processing
DZ2535A1 (en) 1997-06-20 2003-01-08 Exxon Production Research Co Advanced process for liquefying natural gas.
US5992175A (en) 1997-12-08 1999-11-30 Ipsi Llc Enhanced NGL recovery processes
TW477890B (en) 1998-05-21 2002-03-01 Shell Int Research Method of liquefying a stream enriched in methane
US6116050A (en) 1998-12-04 2000-09-12 Ipsi Llc Propane recovery methods
US6119479A (en) 1998-12-09 2000-09-19 Air Products And Chemicals, Inc. Dual mixed refrigerant cycle for gas liquefaction
US6347532B1 (en) * 1999-10-12 2002-02-19 Air Products And Chemicals, Inc. Gas liquefaction process with partial condensation of mixed refrigerant at intermediate temperatures
US6308531B1 (en) * 1999-10-12 2001-10-30 Air Products And Chemicals, Inc. Hybrid cycle for the production of liquefied natural gas
US6401486B1 (en) 2000-05-18 2002-06-11 Rong-Jwyn Lee Enhanced NGL recovery utilizing refrigeration and reflux from LNG plants
WO2001088447A1 (en) 2000-05-18 2001-11-22 Phillips Petroleum Company Enhanced ngl recovery utilizing refrigeration and reflux from lng plants
DE10027903A1 (en) * 2000-06-06 2001-12-13 Linde Ag Recovery of a C2+ fraction from a hydrocarbon feed, especially natural gas, comprises fractionation in a column with a C3+ reflux stream
US6405561B1 (en) * 2001-05-15 2002-06-18 Black & Veatch Pritchard, Inc. Gas separation process
DE10233410A1 (en) * 2002-07-23 2004-02-12 Linde Ag Process for liquefying a hydrocarbon-rich stream with simultaneous recovery of a C3 / C4-rich fraction

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN103265987A (en) * 2013-06-05 2013-08-28 中国石油集团工程设计有限责任公司 Process device and method for removing heavy hydrocarbon in natural gas by adopting LPG (Liquefied Petroleum Gas)

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US6662589B1 (en) 2003-12-16
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CN1539930A (en) 2004-10-27

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